Alkylation process



Feb. 18, 1958 H. M. KNIGHT ETAL 2,824,157

' ALKYLATION PROCESS Filed May 29, 1956 vista.

M g. y mum w 0 T M R u now fi m T MZW 00 H. v! E ALKYLATIUN PROCESS Harmon Knight, La Marque, and Joe T. Kelly, Dick- 'inson, Tex., assignors to The American tlil Company, Texas City, Tex., a corporation of Texas Application May 29, 1956, Serial No. 588,073

14 Claims. (Cl. 260-68344) This invention relates to the reaction of isoparafiins or aromatic hydrocarbons and olefins. More particularly it relates to the alkylation of isobutane with ethylene.

I In the petroleum industry today, the octane race has placed a strain on facilities and materials needed to make gasoline meeting present day automotive engine requirements. One of the remaining sources of high octane components is the product of the alkylation of isobutane and ethylene. This alkylation is not easy to carry out, particularly on a large scale. An object of the invention is the alkylation of isoparaffins, particularly isobutane, with olefins, particularly ethylene. Another object is the alkylation of aromatic hydrocarbons with olefins. Other objects will become apparent in the course of the detailed description.

The alkylation of isoparaffins or aromatic hydrocarbons with olefins is carried out in the presence of a novel catalyst pair. One member of the catalyst pair is boron trifluoride. The other member of the catalyst pair is a metal borate hydrate, that is, a metal borate containing Water ofhys dration. Although the second component of the catalyst pair is spoken of as a metal borate hydrate, it is believed thatthe solid member is more properly a complex of the hereinafter defined metal borate hydrate and BF;,; the B1 is believed to complex with some or all of the hydrate water present in the metal borate hydrate. More than the amount of B1 needed to complex the water of hydration is necessary to obtain the desired catalytic effect.

Boron trifluoride is one member of the catalyst pair. Commercial grade anhydrous BF is suitable for use as one mern ber of the catalyst pair. I I

The other member of the catalyst pair, hereinafter spoken of as the solid member, is a metal borate hydrate, i. e., a metal borate salt containing Water of hydration. The salt may be used as a fine powder, as pellets, or may be supported on a solid carrier such as alumina, charcoal, silica gel, silicon carbide, etc. Not all metal borates which contain water of hydration are suitable, nor are all metal ions suitable. The particular borate salt hydrates are colbalt borate, aluminum pentaborate and nickelous pentaborate. In determining the effective members, it has been considered that the catalyst pairs which did not produce a yield, on a weight percent basis on ethylene charged, when isobutane and ethylene were contacted, of

100% or more, were unsuitable. II

. It is necessary that the above-defined metal salts contain hydrate water. The anhydrous salts do not have arty promotional effect on the activity of BF In those cases wherein a salt may exist in forms having various amounts of water of hydration present, it is not necessary that any particular hydrate be used. Apparently it is necessary only that some water of hydration be present.

The BF and the defined salt react to form a solid material containing complexed BF When the salt hydrate andBF are contacted in a closed vessel, the BF, partial pressure drops very rapidly at first and then gradually approaches a constant value. It appears that avery 2,824,157 Pat nted Feb. 1s, 1ss s rapid reaction between the BE, and some of the water of hydration takes place. This initially rapid reaction is then followed by a relatively slow reaction between the remaining molecules of hydrate water and additional B1 It appears that when the salt hydrate is exposed tOBF even in the presenceof hydrocarbon reactants, eventually all of the water of hydration will become associated with BF on about a 1 mole of BB, per mole of hydrate water basis.

A complex of the defined salt hydrate and BE; is not an effective catalyst for the alkylation in the absence of free-BF Free-B1 is who understood as BF existing in the reaction zone which is not'complexed with the defined metal salt-hydrate. As soon as the salt hydrate has complexted with some BF the beneficial catalytic effect exists. I Thus free-BB may exist in the reaction zone, as evidenced by the formation of alkylate, even though all of the hydrate Water has not been complexed. In a batch system, wherein less BB, is present than is theoretically required to complex all the Water of hydration present in the salt hydrate, eventually no alkylation will occur as charge is added, since all of the BF will become complexed.

In general, the process is carried out utilizing an amount of B1 Which is in excess of that required to complex with all the hydrate waterpresent in the contacting zone, namely, in excess of about 1 mole of BF;; per mole of hydrate water present. More than the minimum amount of free-8P is beneficial, in fact, the yield of alkylate increases rapidly with increase in free-BF, present, up to a maximum amount. The amount of free-BF used is dependent somewhat upon the reactants themselves. However, when reacting isoparafiins and olefins, the free- BF usage is desirably, set out on a BF to olefin weight ratio, of at least about 0.2. In other words, at least about 0.2 lb. of free-B1 per lb. of olefin charged. to the alkyla,- tion zone is desirable. About 1.5 parts by weight of free-BF per part of olefin charged appears to be about the desirable .maximurnusage of BF It is preferred to use between about 0.35 and lpart by weight of free-B1 per part by weight of olefin when utilizing the lower molecular weight olefins, such as ethylene and propylene.

The process may be carried out at any temperature below the temperature at which the salt hydrate decomposes, that is, loss of all its water of hydration. The temperatures of operation may be as low as -20 C. or even lower. Temperatures as high as 150" C. and even higher may be used with some of the salt hydrates which have relatively high decomposition temperatures. More usually the temperature of operation will be between about 0 C. and C. Lower temperatures appear to favor the formation of the hydrocarbons having 6 to 7 carbon atoms. It is preferred to operate at a temperature between about 25 C. and 40 C.

Sufiicient pressure is maintained on the system to keep a substantial portion of the hydrocarbons charged in the liquid state. The process may be carried out at relatively low pressures, for example, 100 p. s. i., or it may be car ried out at elevated pressures, for example, 2000 p. s. i.. or more. In general, pressures will be between about 200 and 1000 p. s. i. and preferably between about 300 and 600 p. s. i.

The contacting of the isoparatfin or aromatic hydrocar bon and the olefin in the presence of the defined catalyst pair is continued until an appreciable amount of alkylate has been formed. In batch reactions, it is possible to convert essentially 100% of the olefin by a sufiiciently long period of, contacting. When operating in a continuous flow system, it may be desirable. to have a time of contacting such thatsubstantial amounts of olefin are not converted and obtain the complete conversion of the olefin by a recycle operation. The time of reaction will be determined by the type of hydrocarbons charged, the ratio of isoparatlin or aromatic to olefin, the degree of mixing in the contacting zone and the catalyst usage. A few tests will enable one to determine the optimum time of contacting for the particular system of operating conditions being tried.

The reactants in the hydrocarbon charge to the alkylation process are isoparaffin, or aromatic and olefin. The olefin contains from 2 to about 12 carbon atoms. Examples of suitable olefins are ethylene, propylene, butene-2, hexene and octene; in addition to these, the olefin polymers obtained from propylene and/ or butylene are also suitable for use in the process, such as codirner, propylene trimer, propylene tetramer and butylene trimer. It is preferred to operate with ethylene or propylene.

The aromatic hydrocarbons must be alkylatable by the particular olefin used. it is self-evident that an aromatic hydrocarbon which contains alkyl substituents positioned so that steric hindrance would prevent or greatly reduce the possibility of alkylation with the particular olefin should not be subjected to the process. Examples of particularly suitable aromatic hydrocarbons are benzene, toluene, xylene, trimethylbenzenes, and the other alkyl analogues, such as propyl and butyl; the naphthalene aromatic hydrocarbons, such as the mono and disubstituted methylnaphthalenes.

The isoparaflin reactant is defined as a parafiinic hydrocarbon which has a tertiary hydrogen atom, i. e., paraffins which have a hydrogen atom attached to a tertiary carbon atom. Examples of these are isobutane, isopentane (Z-methyIbutane), Z-methylpentane, Z-methylhexane, 3-methylhexane, 2,3-dimethylbutane (di-isopropyl) and 2,4-dirnethylhexane. Thus the isoparafiins usable as one reactant in the process contain from 4 to 8 carbon atoms.

In the iscparafiin-olefin system, the alkylation reaction is more favored as the mole ratio of isoparaifin to olefin increases. In general, the isoparafiin to olefin mole ratio in the hydrocarbon charge should be at least 1. More than this amount is good and it is desirable to have an isoparafiin to olefin ratio between about 2 and 25 and in some cases more, for example, as much as 50. It is preferred to operate with an isoparaffin to olefin mole ratio of between about and 15.

The presence of non-reactive hydrocarbons in the hydrocarbon charge is not detrimental unless the reactants become excessively diluted. For example, the isoparaifin may also contain isomers of the normal configuration. The olefins may contain paralfins of the same carbon number. Mixtures of two or more isoparaffins or two or more aromatic hydrocarbons, or two or more olefins ma be charged. In general, when a particular poduct distribution is desired, it is preferable to operate with a single isoparaifin and a single olefin, for example, technical grade isobutane and ethylene, both of about 95% purity.

The reactants may be mixed together before they are charged into the reactor. Cr, they may be charged into the reactor separately. Or, a portion of the olefin may be blended with the isoparafiin or aromatic before introduction into the reactor and the remainder of the olefin injected into the reactor. The charge may be introduced all at one point into the reactor or it may be introduced at two or more points. The alkylation reaction is somewhat exothermic and temperature control is facilitated by iutroductingtl'ie olefin into the reactor at more than one point.

The BB, member of the catalyst pair may be premixed with the isoparafiin and olefin before introducing these into the reactor but this should not be done when an extremely reactive system such as isobutanes and butylene or aromatic hydrocarbons and olefins are being used; or when an olefin that is very rapidly polymerizable, such as isobutylene, is being used. The BP may be blended with the isoparafiin reactant and introduced into the reactor with this member when the isoparafiin and the olefins are liquid and a gas, or two liquids.

a being introduced separately. The B1 may also be introduced directly into the reaction zone independently from the hydrocarbons charged. The 3P may be introduced into the reactor at a single point or at several points to help control temperature and reaction rate.

The reactor may be a vessel providing for a batch-type reaction, i. e., one wherein the desired amount of isoparalfin or aromatic and olefin are charged to a closed vessel containing the catalyst pair and the vessel then maintained at the desired temperature for the desired time. At the end of this time, the hydrocarbon product mixture and unreacted materials are withdrawn from the vessel and processed to separate the alkylate product from the unreacted materials and lower and higher molecular weight materials. The reactor may be a fixed bed operation wherein the reactants and free-5P are flowed through the bed of the hydrate salt member of the catalyst pair, the spaced velocity being controlled so that the desired amount of reaction is obtained during the passage of the reactants through the bed of hydrate salt. Under some conditions, a moving bed of hydrate salt may be utilized. In still another set of circumstances, a fluidized bed of hydrate salt may be utilized with the incoming stream of reactants providing the energy for the fluidization of the solid hydrate salt. Other methods of operation common in the catalytic refining aspects of the petroleum industry utiliz ing solid catalyst may be readily devised.

It has been pointed out that the solid member of the catalyst pair is really a complex of the metal salt hydrate and SP the B1 apparently reacting with the Water of hydration. The complex may be preformed, by exposing the salt hydrate to BE; for a time sufiicient to introduce some BP into the solid component or even enough to complex all of the water of hydration; this being done before the reactants are introduced into the reaction zone or even before the solid member of the catalyst pair is positioned in the reaction zone. The complex may be formed in situ during a batch-type reaction. In the batch-type operation, it is convenient to introduce all the BF into the reaction vessel at once. This amount of BP is suflicient not only to complex with the Water of hydration but also provide the desired amount of free- BF In a flow system, the solid member may be prepared in situ by charging fresh hydrate salt to the reaction zone and forming the complex during the initial passage of reactants and BF over the salt hydrate. Some alkylation reaction occurs even though the salt hydrate has not takenup sufficient SP to complex all the water of hydration. As the flow of reactants and E1 continues over the solid member, eventually the salt hydrate will become saturated with respect to BF At this time, the amount of BF introduced into the reaction Zone should be cut back to that amount of free-BF desired, under this particular set of operating conditions.

The illustrative embodiment set out in the annexed figure forms a part of this specification. It is pointed out that this embodiment is schematic in nature, that many items of process equipment have been omitted, since these may be readily added by those skilled in this art and that this embodiment is only one of many which may be devised, and that the invention it is not to be limited to this particular embodiment.

In this embodiment, it is desired to produce a high yield of di-isopropyl for use as a blending material for gasoline. Ethylene from source 11 is passed by Way of line 12 into mixer 13. Liquid isobutane from source 14 is passed byway of lines 16 and 1'7 into mixer 13. Both the ethylene and the isobutane are about purity, the remainder being n-butane and ethane, with trace amounts ofother components found in materials derived from petroleum refining sources. Mixer 13, in this instance, is a simple orifice-type mixer suitable for intermingling a Recycle isobutane from line 18 is passed by way of line 17 into mixer 13. In

this embodiment, the molar ratio of isobutane to ethylene 13,6: r

' From mixer 13, the blend of isobutane and ethylene is passed by way of line 19, through heat exchanger 21, where the temperature of the blend is adjusted to 30 C. The temperature of the blend leaving exchanger 21 is somewhat lower than the reaction temperature, since there is a heat rise in the reactor due to exothermic reaction. From exchanger 21, thestream of isobutane and ethylene is passed by way of lines 22 and 23 into the top of reactor 24.

Boron trifluoride is passed from source 26 by way of valved line 27 and line 28 into line 23, where it meets the stream of isobutane and ethylene. If desirable, a mixer may be introduced into line 23 to. insure complete intermingling of the BF and the hydrocarbon charged. Recycle BF is introduced from line 29 by way of lines 28 and 23. In this embodiment, the salt hydrate is completely complexed with respect to BE, and only the necessary free-BF is introduced by way of line 28. The weight ratio of free-BF from line 28 to ethylene present in line 23 is 1.1.

Reactor 24 is shown as a shell and tube type vessel. Hydrate salt is contained in the tubes 31. The alumina balls 32 and 33 are positioned above and below the headers in the reactor 'tomain'tairi the hydrate salt within the tubes. In order to maintain the temperature in the reactor at substantially-35 (3., water is introduced into the shell side by way ot line 36 and is withdrawn by way of line 37.

In this embodiment, the reactor was charged with nickel pentaborate containing 4 moles of water of hydration per mole of salt. The hydrate salt was preformed into pellets about one-eighth inch in diameter and about oneeighth inch in height. Some silica was present to act as a lubricant in the extrusion of the pellets. The salt hydrate was contacted with BF in an amount such that all of the water of hydration was complexed with B1 This operation was carried out before reactants were introduced into the reactor. The reactor pressure was maintained at 600 p. s..i. This permits maintaining the isobutane and substantially all of the ethylene in the liquid state.

The product hydrocarbon mixture is passed out of reactor 24 by way of line 41. This stream contains the alkylate product, unreacted isobutane, a small amount-of unreacted ethylene and pentanes as well as BF The stream from line 41 is passed into gas separator 42'where the BF isobutane, some pentanes and some alkylate product are taken overhead by way of line 43. The material taken overhead from the separator 42 is passed into fractionator 44.

Fractionator 44 is adapted to separate the BF as a gas, the isobutaneas a liquid and the higher boiling materials as a bottoms product. Fractionator 44 is provided with an internal reboiler 46 and an internal condenser 47. BE; and unreacted ethylene are taken overhead from fractionator 44 by way of line 48 and may be passed out of thesystem by way of 'valved line 49. Thernaterial fromline-49 may be-periodically passed to a BF purification operation to removeInon-condensable inert gases which build up in the system. Ordinarily the stream from line 48 is recycled by way. of valved lines 29 and lines 28 and23. to reactor 24.

Isobutane is withdrawn as a liquid stream by way of line 51. andis recycled by way of lines 18 and 17 to mixer 13- for reuse in .the process. Bottoms product from fractionator 44 is withdrawn by way of line 52 and may be passed to storage or further processing by way of valyedline .53.. This stream from line 52 consists substantially of isope'ntaneQ Some unaturated C hydrocarbonsare also present and also a small amount of higher boiling alkylate material.

llhegliquids separated in gas separator 42 are passed by way.of ,line 56 into fractionator57. The bottoms prodnot from fractionator 44 may be passed by way of valved line 58 and line56 into fractionator 57 for complete removal of thealliylate material. In this embodiment, the

substantially of isopentane and some unsaturated C material. This material may be used as a high octane blending stock for the production of motor gasoline of the desired 1 velatili ty, characteristics.

The alkylate product herein is considered to be that. boiling above the pentane range and boiling below. themaximum temperature usable in motor gasoline. In general, a 415- F.- endpoint alkylate isblendable into motor gasoline without adverse effect in a specification calling for a 400 F. gasoline endpoint. Thus the alkylate product is considered to be the material boiling between about the lower limit of the hexane range and 415 F. in the ASTM distillation procedure.

A considerable difierence. exists between the, octane number of the C fraction of the alkylate product and the higher boiling material. The C fraction, which boils from about 110 to 170 F., has an F-l octane number of 101. The C material has an octane number which ranges between about and idepending somewhat on the fractionation.

Light alkylate, which includes all the C material and some of the C material, is withdrawn from fractionator 57 by way of line 66. Heavy alkylate, which includes most of-the C and material boiling up to 415 F., is withdrawn from fractionator 57 by way of line 67. A small amount of higher boiling bottoms is withdrawn by way of line 68.

In general, the C fraction of the alkylate product will contain from about 86 to about 90 mole percent of diisopropyl, (2,3-dimethylbutane) the C product. Generally, only trace amounts ofnhexane are present.

The results obtainable by the process of the instant invention are set out in illustrative runs below. In Tables I and II, there are set out results in the testing of various metal borate hydrates by 'means of batch operation. In these runs, the tests were carried out under what are more or less standard conditions, namely, a 4-liter carbon steel bomb was dried overnight in a stream of hot air at C. The salt to be tested (90 grams) was charged to the bomb as a powder and the bomb was evacuated. One kilogram of a dry blend of ethylene and isobutane was added and then BF (90, grams) was pressured in. The charged bombs were placed in a rocker and allowed to rock for 20 hours. At the end of this time a liquid sample was drawn through a bomb containing activated alumina (to remove dissolved BF and salt par ticles). This sample was submitted for Podbielniak distillation. A C cut from the Podbielniak distillation was analyzed by mass spectrometer. In some cases after sampling, the remaining major portion of the product was debutanized on an Oldershaw column and then fractionated on a packed column.

In Table I, run No. 1 was carried out as described above except that no salt was present in the bomb. The results show that only 34% of depentanized alkylate product was obtained by the use of BF alone as the catalyst. Run No. 2 used BFg and cobalt borate hydrate, in the form of ZCoB O CoO I-I JH O, produced of alkylate. Runs 3 and 4 show the effect of using BF and nickel pentaborate hydrate and aluminum penta: borate hydrate respectively; these were very good pro moters..

Z-methylpentane and S-methylpentane represent substantially the remainder of In Table No. II, there are set out the results of testing various metal borate hydrates. These data were obtained under the approximate standard conditions utilized in bomb work. These standard conditions are place, in the presence of a catalyst comprising essentially (i) a metal salt containing water of hydration, the metal salt being selected from the class consisting of cobalt borate, aluminum pentaborate and nickelous pentaborate,

approximately: Isobutane-ethylene mole ratio, 2.5; BF and boron 'lfiflllofidti, Said a bfiing Present in an ethylene weight ratio, 0.7; 20 hours contacting time, ternamount in eacess of one mole per mole of hydrate water perature range, 2035 C. and an initial pressure of Present 111 5211Cl Salt, remflvlng a Product hydrocarbon 1111K- about 350 p. s. i. g. These runs show that only one lure from Sald Contactmg Zone and an alkylate Y borate hydrate was effective in promoting BF for iso- Carbon Product Separated from 531d mlXtuTeparafiin-olefin alkylation. 10

TABLE I Cobalt borate and two pentaborates Run No 1 2 3 4 te None 2COBzO4.COOzHz.ZHzO NlBro0m.4-5H2O 2( l0 lll)3' Condltious:

Isobutane/Ethylene (molar) 3.0 2. 4 3.3 2.1 Hydrocarbon/Salt (weight) 11. 6 11.4 27.9 BF lEthylene (weight). 0. 7 0. 7 0.8 0.7 Time, Hours 20 20 20 20 Temperature, C -35 20-30 2535 25-30 Pressure (Range), p. s. i. g 300 250-185 272-175 315-205 z i l li l t (D t d) y a e open anize 1 wt. percent)Pentanes 0 16 25 26 Ethylene Converted, Percent 96 82 89 1 Podbielniak and mass spectrometer analyses, based on ethylene charged. 2 88% 2,3-dimethylbutane.

TABLE II Various borate hydrates Run No 2 5 6 7 8 9 Metal Ion Present Cobalt Alumi- Cadrni- Copper Lead Manganum um nese Moles of Water of Hydration x :r 2 1 1 1 Ethylene Converted, Percent- 96 70 70 24 Alkrlate (Wt. Percentfi:

Isopentane 16 31 0 0 Hexanes 78 53 14 6 7+ 92 43 18 Total (05 Free) 170 98 57 44 10 24 1 Based on ethylene charged.

Thus having described the invention what is claimed is: 3. The process of claim 2 wherein said isoparaflin is 1. An alkylation process comprising contacting (a) an alkylatable feed hydrocarbon from the class consisting of (1) isoparatfin having from 4 to 8 carbon atoms and (2) aromatic hydrocarbon and (b) an olefin having from 2 to 12 carbon atoms, in the presence of a catalyst comprising essentially (i) a metal salt containing water of hydration, said metal salt being from the class consisting of cobalt borate, aluminum pentaborate and nickelous pentaborate, and (ii) B1 said 8P being present in an amount in excess of about 1 mole per mole of water of hydration in said salt, at a temperature between about 30 C. and a temperature susbtantially below the temperature at which said hydrate salt decomposes, and at a pressure suflicient to maintain a substantial portion of said reactants in the liquid state, and separating a hydrocarbon product mixture containing alkylate product of said feed hydrocarbon and said olefin.

2.. An alkylation'process wherein an isoparafiin having from 4 to 8 carbon atoms and an olefin having from 2 to 12 carbon atoms are contacted, in a molar ratio of isoparaffin to olefin between about 2 and 50, at a temperature between about -2() C. and 150 C. and a pressure between about 100 and 2000 p. s. i., said pressure being at least sufficient to keep a substantial portion of said reactants in the liquid state, for a time sufiicient to permit an appreciable amount of alkylation reaction to take isobutane.

4. The process of claim 2 wherein said isoparafiin is diisopropyl.

5. The process of claim 2 wherein said olefin is ethylene.

6. The process of claim 2 wherein said olefin is propylene tetramer.

7. The process of claim 2 wherein said salt hydrate is 2CoB O .CoO H .xI-1 O.

8. The process of claim 2 wherein said salt hydrate is aluminum pentaborate hydrate.

9. The process of claim 2 wherein said salt hydrate is nickelous pentaborate hydrate.

10. The process of claim 2 wherein said temperature is between about 25 C. and 40 C.

11. The process of claim 2 wherein the BF is present in an amount, in excess of 1 mole per mole of hydrate water, such that the free-BF to olefin weight ratio is between. about 0.2 and 1.5.

12. An alkylation process which comprises contacting isobutane and ethylene in a molar ratio of isobutane, to ethylene between about 2 and 25 at a temperature between about 20 C. and C. at a pressure between about 200 and 1000 p. s. i., said pressure being sufficient to keep a substantial portion of said reactants in the liquid state for a time sufiicient to permit an appreciable amount of alkylation reaction to take place, in the presence of a catalyst pair comprising essentially (a) a salt-BF complex consisting of a metal salt containing water of hydration, the metal salt being selected from the class consisting of cobalt borate, aluminum pentaborate and nickelous pentaborate, and about 1 mole of B1 per mole of hydrate water present in said salt and (b) boron trifluoride in an amount such that the weight ratio of free-BF to, ethylene charged is at least about 0.2, removing product hydrocarbon mixture containing alkylate product from said 1 contacting zone and separating alkylate hydrocarbon product from unreacted isobutane and ethylene.

13. The process of claim 12 wherein said temperature is between about 25 C. and 40 C.

14. The process of claim 12 wherein said free-BF ethylene Weight ratio is between about 0.35 and l.

References Cited in the file of this patent UNITED STATES PATENTS 

1. AN ALKYLATION PROCESS COMPRISING CONTACTING (A) AN ALKYLATABLE FEED HYDROCARBON FROM THE CLASS CONSISTING OF (1) ISOPARAFFIN HAVING FROM 4 TO 8 CARBON ATOMS AND (2) AROMATIC HYDROCARBON AND (B) AN OLEFIN HAVING FROM 2 TO 12 CARBON ATOMS, IN THE PRESENCE OF A CATALYST COMPRISING ESSENTIALLY (I) A METAL SALT CONTAINING WATER OF HYDRATION, SAID METAL SALT BEING FROM THE CLASS CONSISTING OF COBALT BORATE, ALUMINUM PENTABORATE AND NICKELOUS PENTABORATE, AND (II) BF3, SAID BF3 BEING PRESENT IN AN AMOUNT IN EXCESS OF ABOUT 1 MOLE PER MOLE OF WATER OF HYDRATION IN SAID SALT, AT A TEMPERATURE BETWEEN ABOUT -30* C. AND A TEMPERATURE SUBSTANTIALLY BELOW THE TEMPERATURE AT WHICH SAID HYDRATE SALT DECOMPOSES, AND AT A PRESSURE SUFFICIENT TO MAINTAIN A SUBSTANTIAL PORTION OF SAID REACTANTS IN THE LIQUID STATE, AND SEPARATING A HYDROCARBON PRODUCT MIXTURE CONTAINING ALKYLATE PRODUCT OF SAID FEED HYDROCARBON AND SAID OLEFIN. 